JPH06346389A - Method for deinking and apparatus therefor - Google Patents
Method for deinking and apparatus thereforInfo
- Publication number
- JPH06346389A JPH06346389A JP15461093A JP15461093A JPH06346389A JP H06346389 A JPH06346389 A JP H06346389A JP 15461093 A JP15461093 A JP 15461093A JP 15461093 A JP15461093 A JP 15461093A JP H06346389 A JPH06346389 A JP H06346389A
- Authority
- JP
- Japan
- Prior art keywords
- bubbles
- air
- pressure
- deinking
- zone
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/64—Paper recycling
Landscapes
- Paper (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は脱インキ方法及び装置に
関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a deinking method and apparatus.
【０００２】[0002]
【従来の技術】従来の脱インキ方法として、ＰＤＭ（加
圧型脱インキモジュール）について説明すると、図６に
示すように、ケーシング６の円周方向に設けられた複数
の空気注入部１から圧縮空気を吹き込んで、ドーナツ状
の空気室を形成させると共に、供給空気の一部を加圧下
で原料２中に溶解させると同時に、同空気室に対する原
料流の機械的な剪断作用により気泡を発生させる。図５
は従来のＰＤＮの１部切截全体図を示し、エアを溶解さ
せるエアレーションゾーンＡに続いて、ミキシングゾー
ンＢと分離ゾーンＣが形成されており、ミキシングゾー
ンＢでは、図７に示すように数段の拡大急縮流路５が形
成されている。2. Description of the Related Art A PDM (pressurized deinking module) will be described as a conventional deinking method. As shown in FIG. 6, compressed air is supplied from a plurality of air injecting portions 1 provided in a circumferential direction of a casing 6. Is blown in to form a donut-shaped air chamber, and at the same time, a part of the supply air is dissolved in the raw material 2 under pressure, and at the same time, bubbles are generated by the mechanical shearing action of the raw material flow against the air chamber. Figure 5
Shows a partial cutaway view of a conventional PDN, in which a mixing zone B and a separation zone C are formed following an aeration zone A for melting air. In the mixing zone B, as shown in FIG. A stepwise expansion / contraction channel 5 is formed.
【０００３】さて図７における拡大流路での圧力損失に
よる圧力低下作用により、原料中の溶解空気が気泡とな
って疎水性のインキ粒子の表面上に析出する。即ち、数
段の拡大急縮流路５での加減速流れと、マイクロタービ
ュレンスにより、微細気泡を含む幅広いサイズ分布の気
泡とインキ粒子の衝突と付着が、高度に達成される。次
に分離ゾーンＣでは、インキ粒子を付着した気泡を気液
界面に向けて上昇させ（Ｄの範囲）て、液面上にインキ
を含有した泡を形成させる。この時分離ゾーンＣで原料
のフローパターンを制御して適度な乱流を維持すること
により、繊維の泡への混入を抑制し、繊維の歩留りを向
上させる。次に界面上のフロスは、リジェクト３として
排出され、他はアクセプト４として次の段のＰＤＭ装置
に導入される。なお、従来の場合、エアレーションゾー
ンの滞留時間は 0.1秒以下である。By the pressure lowering action due to the pressure loss in the enlarged flow passage in FIG. 7, the dissolved air in the raw material becomes bubbles and deposits on the surface of the hydrophobic ink particles. That is, due to the acceleration / deceleration flow in the several stages of expansion / contraction channels 5 and the microturbulence, the collision and adhesion of the ink particles and the bubbles having a wide size distribution including fine bubbles are highly achieved. Next, in the separation zone C, bubbles containing ink particles are raised toward the gas-liquid interface (range D) to form bubbles containing ink on the liquid surface. At this time, by controlling the flow pattern of the raw material in the separation zone C and maintaining an appropriate turbulent flow, the mixing of fibers into bubbles is suppressed, and the yield of fibers is improved. Next, the floss on the interface is discharged as reject 3 and the other is accepted as accept 4 and introduced into the PDM device in the next stage. In the conventional case, the residence time in the aeration zone is 0.1 second or less.
【０００４】[0004]
【発明が解決しようとする課題】近年回収古紙の上質紙
への再利用を目指すことが盛んになり、白色度を従来以
上に向上させることが望まれている。このため脱インキ
装置において、特に１０μｍ以下の微細なインキ粒子を
除去する必要が生じている。浮選機にて微細なインキ粒
子を除去するためには、インキ粒子の気泡への付着のチ
ャンスを増大させることが先ず必要であり、空気吹込量
の増大、滞留時間の延長、気泡の微細化などの対策がと
られている。また微細なインキを除去するためには、細
かい泡を作ることが必要であることは従来より知られて
おり、例えばｘ（μｍ）の粒子径のインキを取るために
は、５×ｘ（μｍ）以下の直径の気泡を発生させること
が好ましい。しかし小気泡は浮上速度が小さく、分離性
が余りよくない。本発明は浮上分離よりも強力な遠心力
を利用することにより、分離性に優れた脱インキ方法及
び装置を提供せんとするものである。In recent years, it has become more and more popular to aim to reuse recovered recovered paper as high-quality paper, and it is desired to improve the whiteness more than ever before. Therefore, it is necessary to remove fine ink particles of 10 μm or less in the deinking device. In order to remove fine ink particles with a flotation machine, it is first necessary to increase the chances of ink particles adhering to the bubbles, increasing the amount of air blown in, extending the residence time, and making the bubbles smaller. Such measures are taken. Further, it has been known that it is necessary to form fine bubbles in order to remove fine ink. For example, in order to remove ink having a particle size of x (μm), 5 × x (μm ) It is preferable to generate bubbles having the following diameters. However, small bubbles have a low floating speed, and their separability is not very good. The present invention intends to provide a deinking method and apparatus excellent in separability by utilizing a centrifugal force stronger than the floating separation.
【０００５】[0005]
【課題を解決するための手段】このため本発明は、回収
古紙を含むパルプ原料液に、１〜１０kg/cm2Ｇの加圧力
で空気を注入し、１〜４秒間保持溶解した後ミキシング
ゾーンにて気泡を発生させ、次いで同気泡を遠心分離す
るようにしてなるもので、これを課題解決のための手段
とするものである。また本発明は、回収古紙を含むパル
プ原料液に空気を加圧注入する手段と、同注入空気の圧
力を保持しつつ前記原料液に注入した空気を溶解させる
滞留ゾーンと、同滞留ゾーンに続き気泡を発生させるミ
キシングゾーンと、同ミキシングゾーンで発生した気泡
を分離浮上させる遠心分離ゾーンを設けてなるもので、
これを課題解決のための手段とするものである。Therefore, according to the present invention, air is injected into a pulp raw material liquid containing recovered waste paper at a pressure of 1 to 10 kg / cm 2 G, and the mixture is held and dissolved for 1 to 4 seconds and then mixed in a mixing zone. To generate bubbles and then to centrifuge the bubbles, which is a means for solving the problem. The present invention further comprises means for pressurizing and injecting air into the pulp raw material liquid containing recovered waste paper, a retention zone for dissolving the air injected into the raw material liquid while maintaining the pressure of the injection air, and a continuation of the retention zone. A mixing zone for generating bubbles and a centrifugal zone for separating and floating bubbles generated in the mixing zone are provided.
This is a means for solving the problem.
【０００６】[0006]
【作用】小粒径のインキを除去するには、より多くの小
径の泡を必要とする。小粒径の泡を発生させるには、加
圧溶解が最もよく使用される。また分離性について、重
力分離では小径の気泡は極めて浮上しにくいので、本発
明では遠心力を利用して気泡を集合化させることによ
り、細かいインキ粒子を中心に除去性の向上を図ること
ができる。[Function] In order to remove the ink having a small particle diameter, more bubbles having a smaller diameter are required. Pressure dissolution is most often used to generate small particle size bubbles. Regarding the separability, since bubbles of small diameter are extremely difficult to float by gravity separation, the present invention can improve the removability centering on fine ink particles by assembling the bubbles by utilizing centrifugal force. .
【０００７】[0007]
【実施例】以下本発明を図面の実施例について説明す
る。先ず小粒径（１０μｍ以下）のインキを除去するた
めには、より多くの小径の泡を必要とする。小粒径の泡
を発生させるには、様々な方法が考えられるが、加圧溶
解が現実には最もよく使用される方法の１つである。即
ち、加圧下で飽和溶解量の空気を溶かし、圧力の低い領
域で小径の気泡を発生させる。本発明者らが直管を用い
て空気の溶解量を調べた所、滞留時間に最適値があるこ
とが分かった。即ち、溶解するのには時間が必要である
が、余り時間が長くなると、直管内の圧力損失のために
絶対圧が下がって、溶解空気量がヘンリーの法則に従っ
て低下する。また分離性については、重力（浮上）分離
では、小径の気泡は極めて浮上し難い。そこで遠心力を
利用して、気泡を集合化させるようにして分離する。但
し、遠心力もかけすぎると、一度合体したインキと気泡
が分離される可能性があるため、対象とする古紙原料に
応じて適当な遠心力を選ぶ必要がある。DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below with reference to the embodiments of the drawings. First, in order to remove the ink having a small particle size (10 μm or less), more bubbles having a smaller diameter are required. Although various methods can be considered for generating bubbles having a small particle size, pressure dissolution is one of the most commonly used methods in reality. That is, the saturated dissolved amount of air is melted under pressure, and small-diameter bubbles are generated in the low pressure region. When the present inventors investigated the amount of dissolved air using a straight pipe, it was found that the residence time had an optimum value. That is, it takes time to melt, but if the time is too long, the absolute pressure decreases due to the pressure loss in the straight pipe, and the amount of dissolved air decreases according to Henry's law. Regarding the separability, bubbles of small diameter are extremely difficult to float by gravity (floating) separation. Therefore, the centrifugal force is used to separate the bubbles so as to aggregate them. However, if too much centrifugal force is applied, the ink and the air bubbles that have once been combined may be separated, so it is necessary to select an appropriate centrifugal force according to the target waste paper material.
【０００８】図１に本発明のフロー図を示す。先ず円管
を流れるパルプ原料２に、空気を図６と同様に注入し
た。即ち、加圧約２kg/cm2Ｇの下で空気を注入した。パ
ルプ原料２は２秒程度配管７を通って溶解し、更に気泡
とインキを図７と同様な拡大急縮流路５で混合させ、次
いで遠心式分離器８で気体を分離し、中心部付近に集合
した泡とインキの合体物を含むリジェクト３と脱インキ
されたアクセプト４に分離する。また微細気泡の発生の
方法は、次の通りである。即ち、気泡の吹き込み方は従
来と同様であるが、溶解ゾーンを設け、ヘンリーの法則
に従って溶解した空気をミキシングゾーンで析出させる
ものである。なお、気泡分離法としては、重力分離法の
代わりに遠心分離法を使用するものである。FIG. 1 shows a flow chart of the present invention. First, air was injected into the pulp raw material 2 flowing through the circular tube in the same manner as in FIG. That is, air was injected under a pressure of about 2 kg / cm 2 G. The pulp raw material 2 is melted through the pipe 7 for about 2 seconds, and the air bubbles and the ink are mixed in the expansion and contraction flow path 5 similar to that shown in FIG. 7, and then the centrifugal separator 8 separates the gas, near the center part. It is separated into a reject 3 containing a combined product of bubbles and ink and a deinked accept 4. The method of generating fine bubbles is as follows. That is, although the method of blowing bubbles is the same as the conventional method, a dissolving zone is provided and dissolved air is deposited in the mixing zone according to Henry's law. As the bubble separation method, a centrifugal separation method is used instead of the gravity separation method.
【０００９】従来例の場合は浮上分離であるため、下記
のストークスの式によって浮上速度が決まるが、泡径が
小さくなるにつれて、浮上速度は極めて小さくなる。In the case of the conventional example, since the levitation is separated, the levitation speed is determined by the following Stokes' equation, but the levitation speed becomes extremely small as the bubble diameter becomes smaller.
【数１】 ＶH ＝ｇ・ｄ2(ρl −ρP ) ／18μ ‥‥‥ (1) ここで ｄ：泡径（m) ｇ：重力加速度（＝9.8m/s2) ＶH : 浮上速度（m/s) μ：粘度 (kg/m・sec)[Formula 1] V H = g · d 2 (ρ l −ρ P ) / 18μ ‥‥‥‥ (1) where d: bubble diameter (m) g: gravitational acceleration (= 9.8 m / s 2 ) V H : Ascent rate (m / s) μ: Viscosity (kg / msec)
【００１０】例えば粘度が１０-3kg/m・sec(＝１センチ
ポイズ）の場合、５０μｍの泡の浮上速度は1.36mm/sec
であって、極めて小さく、それ以下の泡径では更に浮上
速度は小さくなる。一方本発明の遠心分離法は、分離速
度が以下のようになる。For example, when the viscosity is 10 −3 kg / m · sec (= 1 centipoise), the floating speed of bubbles of 50 μm is 1.36 mm / sec.
However, when the bubble diameter is extremely small, the floating speed becomes smaller. On the other hand, in the centrifugal separation method of the present invention, the separation speed is as follows.
【数２】 Ｖc ＝（ρl −ρP ) ｄ2 ・ ｗ2 ｒ／18μ ‥‥‥ (2) ＝ＶR 2 ／ｇ・ｒ ＶH ここで ｗ：角速度（rad/sec) ｒ：回転半径（m) ＶR ：回転速度（m/sec) ρl , ρP ：液体及び気体の密度 (kg/m3)[Number 2] Vc = (ρ l -ρ P) d 2 · w 2 r / 18μ ‥‥‥ (2) = V R 2 / g · r V H here w: angular velocity (rad / sec) r: Rotation radius (m) V R: speed (m / sec) ρ l, ρ P: density of the liquid and the gas (kg / m 3)
【００１１】仮に (1)式の浮上分離の場合、流体の水平
方向の速度をＶc ＝0.061m/secとし、浮上高さＨ＝ 0.3
14ｍ、浮上所要距離を求めると、粒子径と浮上所要距離
の関係は表１のようになった。In the case of levitation separation of equation (1), the horizontal velocity of the fluid is Vc = 0.061 m / sec, and the levitation height H = 0.3.
When the required flying distance was found to be 14 m, the relationship between the particle diameter and the required flying distance was as shown in Table 1.
【表１】 [Table 1]
【００１２】表１から浮上所要距離を１ｍとすると、限
界の浮上粒子径は１８８μｍとなる。なお、浮上所要距
離は、図５のＤ方向の距離を云う。ところが同一の物性
で、遠心分離法を適用し、ｒ＝ 0.2ｍ、ＶR ＝３m/s と
すると、５０μｍの粒子径で、From Table 1, assuming that the required flying distance is 1 m, the limit floating particle diameter is 188 μm. The required flying distance is the distance in the D direction of FIG. However, when the centrifugal separation method is applied with the same physical properties and r = 0.2 m and V R = 3 m / s, a particle diameter of 50 μm
【数３】Ｖc ＝３2 ／9.8 ×0.2 ×1.36＝6.25mm/sec 0.2／6.25×10-3≦Ｌ／0.061(m/sec) Ｌ＝1.95ｍとなり、この長さだけあれば、５０μｍ以上
の泡径まで除去可能となる。[Equation 3] Vc = 3 2 /9.8 × 0.2 × 1.36 = 6.25mm / sec 0.2 / 6.25 × 10 -3 ≦ L / 0.061 (m / sec) L = 1.95m, and if this length is 50μm or more It is possible to remove up to the bubble size.
【００１３】次に円管を用いて測定した液流れ方向の滞
留時間と、溶存空気量の関係を図２に示す。これより滞
留時間が２秒程度で、溶存空気量がピークとなることが
分かる。この場合は約２〜３秒程度が実用的と考える。
なお、図２で示す破線は、2.0 kg/cm2Ｇ、１８℃での飽
和空気量を示す。また圧力が1.0 kg/cm2Ｇの場合は、滞
留時間３〜４秒がピークとなり、圧力が10.0kg/cm2Ｇの
場合は、１〜2.5 秒となるので、全体を含めて１〜４秒
が下記に示す圧力１〜１０kg/cm2Ｇの範囲で実用的と考
える。なお、遠心力の範囲としては、 (2)式のＶc ／Ｖ
H ＝ＶR 2 ／ｇｒで表わすと、３≦ＶR 2 ／ｇｒ≦２０
が実験的に好ましい。この範囲はＶR 2 ／ｇｒを３以上
に取らないと、浮上分離式に比較して装置をコンパクト
にできないためであり、２０以上とすると一旦泡と合体
したインキが遠心力により分離されるためである。な
お、表１の浮上所要距離とは、円管の底部に泡が存在し
たと仮定して、液面に浮上するのに必要な距離（円管の
流れ方向の長さ）をストークスの式により計算したもの
である。FIG. 2 shows the relationship between the residence time in the liquid flow direction measured using a circular tube and the amount of dissolved air. From this, it can be seen that the amount of dissolved air reaches a peak when the residence time is about 2 seconds. In this case, it is considered that about 2 to 3 seconds is practical.
The broken line shown in FIG. 2 indicates the saturated air amount at 18 ° C. at 2.0 kg / cm 2 G. In addition, when the pressure is 1.0 kg / cm 2 G, the residence time peaks at 3 to 4 seconds, and when the pressure is 10.0 kg / cm 2 G, it becomes 1 to 2.5 seconds. It is considered to be practical within a pressure range of 1 to 10 kg / cm 2 G per second as shown below. The range of centrifugal force is as follows: Vc / V in equation (2)
When expressed by H = V R 2 / gr, 3 ≦ V R 2 / gr ≦ 20
Is experimentally preferable. This range is because if V R 2 / gr is not set to 3 or more, the apparatus cannot be made compact as compared with the floating separation type, and if it is 20 or more, the ink once combined with the bubbles is separated by centrifugal force. Is. Note that the required floating distance in Table 1 is the distance (length in the flow direction of the circular pipe) required to float to the liquid surface, calculated based on the Stokes equation, assuming that bubbles were present at the bottom of the circular pipe. It is calculated.
【００１４】一方圧力の限定範囲は、１kg/cm2Ｇ〜１０
kg/cm2Ｇである。また常圧での空気溶解量をＳ、圧力を
Ｐg(kg/cm2Ｇ) とすると、その圧力での最大の空気溶解
量は、（Ｐg ＋１）×Ｓとなる。故にＰg を余り小さく
すると、空気溶解量が小さくなりすぎるため、常圧の２
倍以上、即ち、Ｐg ＝１kg/cm2Ｇ以上とするのが好まし
い。また圧力が高ければ高い程、原理的には小さい泡を
多数発生させるが、余り多すぎても脱インキへの効果が
上がらなくなるため、実用上は１０kg/cm2Ｇ以下であ
る。On the other hand, the limited range of pressure is 1 kg / cm 2 G to 10
It is kg / cm 2 G. If the amount of air dissolved at normal pressure is S and the pressure is Pg (kg / cm 2 G), the maximum amount of air dissolved at that pressure is (Pg + 1) × S. Therefore, if Pg is made too small, the amount of air dissolved will become too small.
It is preferable that it is more than double, that is, Pg = 1 kg / cm 2 G or more. Further, the higher the pressure is, the more small bubbles are generated in principle, but the effect on deinking will not be enhanced even if it is too much, so that it is practically 10 kg / cm 2 G or less.
【００１５】次に本発明の実施例における第１の具体例
を説明する。同一の原料（新聞古紙）、溶液（水８００
リットルに対して脱墨剤４０ｇ、水酸化ナトリウム84.2
ｇ、珪酸ソーダ６００ｇ、過酸化水素２２９ｇ）で処理
し、これを濃度１％になるように希釈したものを用い
た。処理液量は２８５リットル／min 、空気液比＝２０
％、入力圧力＝２kgf/cm2の場合、ＰＤＭを６段直列に
つないで最終段で測定した脱インキ率を図３のハッチン
グの部分に示す。本発明はハッチングなしの部分であ
る。また脱インキ率はＪＩＳ法に従って手抄紙により濾
過し、その紙を粒子アナライザにより測定した値を用い
た（ＪＩＳ−ＴＡＰＰＩ 紙パルプ試験方法 No.39-8
2)。本発明は前記従来法に対し空気溶解時間を２秒と
り、直径４０cm、長さ２ｍの円管に回転速度３m/sec の
速度を与えるようにした。その結果本発明の方が従来法
よりも、特に１０μｍ以下の粒子径インキの除去性能が
高いことが分かった。Next, a first specific example in the embodiment of the present invention will be described. The same raw material (newspaper waste), solution (water 800
Deinking agent 40 g, sodium hydroxide 84.2 per liter
g, 600 g of sodium silicate, 229 g of hydrogen peroxide) and diluted to a concentration of 1% were used. Treatment liquid volume is 285 liters / min, air-liquid ratio = 20
%, Input pressure = 2 kgf / cm 2 , the deinking rate measured at the final stage by connecting 6 stages of PDM in series is shown in the hatched portion of FIG. The present invention is the part without hatching. The deinking rate was obtained by filtering the paper with handmade paper according to the JIS method and measuring the paper with a particle analyzer (JIS-TAPPI Paper Pulp Test Method No. 39-8).
2). In the present invention, the air dissolution time is set to 2 seconds in comparison with the conventional method, and a circular tube having a diameter of 40 cm and a length of 2 m is given a rotation speed of 3 m / sec. As a result, it was found that the present invention has a higher performance of removing ink having a particle size of 10 μm or less than the conventional method.
【００１６】次に本発明を第２の具体例により説明す
る。この第２具体例は第１具体例と同様の条件で、入口
圧力を３kg/cm2Ｇとしたもので、その時のテスト結果を
図４に示す。図４と図３を比較すると、図４の方が全般
的なインキ除去率は良好になっている。Next, the present invention will be described with reference to a second specific example. In this second specific example, the inlet pressure was 3 kg / cm 2 G under the same conditions as in the first specific example, and the test results at that time are shown in FIG. Comparing FIG. 4 and FIG. 3, the overall ink removal rate is better in FIG.
【００１７】次に図１の装置について説明すると、図１
の空気注入部１は図６の従来の空気注入部１と同一形状
である。図６ではｄ1 ＝７７φ、ｄ2 ＝８７φ、ｄ3 ＝
１３φとなっている。ここでｄ3 の空気注入管１は、ｄ
3 の円周の接線方向に入るようになっている。図１のＦ
の部は、滞留時間が約２秒となるように配置された内径
７７φで、2.2 ｍの長さのパルプとなっている。また図
１のＢ部は、図８に示すように円柱を截頭円錐状に削成
した形状となっており、それを４〜６個連結している。
１例としてｄ4 ＝６８φ、ｄ5 ＝３０φ、ｄ6 ＝７６φ
である。また図１のＤは図９と同一構造で、通常の液体
サイクロンと同様の形状であり、入口配管９は分離器８
に対して接線方向に接続されている。１例としてｄ8 ＝
１１０φ（内径）、ｄ7 ＝６０φ（内径）であり、ｄ9
＝１１０とした。Next, the apparatus shown in FIG. 1 will be described.
The air injecting section 1 has the same shape as the conventional air injecting section 1 in FIG. In FIG. 6, d 1 = 77φ, d 2 = 87φ, d 3 =
It is 13φ. Here, the air injection pipe 1 of d 3 is d
It is designed to enter the tangential direction of the circumference of 3 . F of FIG.
The section is a pulp having an inner diameter of 77φ and a length of 2.2 m arranged so that the residence time is about 2 seconds. Further, as shown in FIG. 8, the portion B in FIG. 1 has a shape in which a column is cut into a truncated cone shape, and 4 to 6 pieces thereof are connected.
As an example, d 4 = 68φ, d 5 = 30φ, d 6 = 76φ
Is. Further, D of FIG. 1 has the same structure as that of FIG. 9 and has the same shape as a normal liquid cyclone, and the inlet pipe 9 is a separator 8
Are tangentially connected to. As an example, d 8 =
110φ (inner diameter), d 7 = 60φ (inner diameter), and d 9
= 110.
【００１８】従来法は図６に示すような空気注入部があ
り、すぐに溶解ゾーンがなくて、図７の拡大急縮流路５
を有するミキシングゾーンがある。なお、この場合の管
径やミキシング部のサイズは、本発明と同様である。ま
た従来法の図５の分離部Ｄの内径は31.4cmであり、長さ
は約1.0 ｍ／段であるが、６段あるので６ｍとなる。こ
こで本発明方法と従来方法を比較すると表２のようにな
る。The conventional method has an air injection part as shown in FIG. 6 and immediately has no melting zone.
There is a mixing zone with. The pipe diameter and the size of the mixing portion in this case are the same as those in the present invention. Further, the inner diameter of the separating portion D in FIG. 5 of the conventional method is 31.4 cm, and the length is about 1.0 m / step, but since there are 6 steps, it becomes 6 m. Table 2 shows a comparison between the method of the present invention and the conventional method.
【表２】 なお、前記第２の具体例は、第１具体例と比較して圧力
を高くし、溶解空気を増やして、微少の泡を多数発生さ
せた時の効果を調べたものである。[Table 2] In the second specific example, the effect when a large number of minute bubbles are generated by increasing the pressure and increasing the dissolved air in comparison with the first specific example is examined.
【００１９】[0019]
【発明の効果】以上詳細に説明した如く本発明では、注
入空気を溶解させる滞留ゾーンを設けることにより、従
来方式に比べて微細径の気泡を多く発生させることがで
き、細かい（１０μｍ以下）インキ粒子の除去性を向上
できる。また本発明は、浮上分離ではなく遠心分離法を
利用するため、微細気泡が分離できない従来法に比較し
て、細かい（１０μｍ以下）インキ粒子を中心に除去性
の向上を図ることができる。As described above in detail, in the present invention, by providing the retention zone for dissolving the injected air, it is possible to generate a large number of bubbles having a fine diameter as compared with the conventional method, and a fine (10 μm or less) ink. The removability of particles can be improved. In addition, since the present invention utilizes the centrifugal separation method instead of the floating separation method, it is possible to improve the removability centering on fine (10 μm or less) ink particles, as compared with the conventional method in which fine bubbles cannot be separated.
【図１】本発明の実施例に係る脱インキ装置のフロー図
である。FIG. 1 is a flow chart of a deinking device according to an embodiment of the present invention.
【図２】本発明の実施例における流れ方向の滞留時間と
溶存空気量との関係を示す線図である。FIG. 2 is a diagram showing the relationship between the residence time in the flow direction and the amount of dissolved air in the example of the present invention.
【図３】本発明におけるインキ粒子サイズとインキ除去
率との関係の１例を示す説明図である。FIG. 3 is an explanatory diagram showing an example of the relationship between the ink particle size and the ink removal rate in the present invention.
【図４】本発明におけるインキ粒子サイズとインキ除去
率との関係の他の例を示す説明図である。FIG. 4 is an explanatory diagram showing another example of the relationship between the ink particle size and the ink removal rate in the present invention.
【図５】従来のＰＤＭの全体側面図である。FIG. 5 is an overall side view of a conventional PDM.
【図６】従来のＰＤＭの気体注入部の断面図である。FIG. 6 is a cross-sectional view of a gas injection part of a conventional PDM.
【図７】従来のＰＤＭの混合部流路を示す側断面図であ
る。FIG. 7 is a side sectional view showing a mixing section flow path of a conventional PDM.
【図８】図７における混合部流路の大径部と小径部寸法
を示す断面図である。8 is a cross-sectional view showing dimensions of a large diameter portion and a small diameter portion of the mixing section flow passage in FIG.
【図９】図６の装置における分離器の詳細図である。9 is a detailed view of the separator in the apparatus of FIG.
１ 空気注入部 ２ 原料 ３ リジェクト ４ アクセプト ５ 拡大急縮流路 ７ 溶解のための配管 ８ 遠心式分離器 ９ 配管 1 Air injection part 2 Raw material 3 Reject 4 Accept 5 Expanded rapid compression flow path 7 Pipe for dissolution 8 Centrifugal separator 9 Pipe
Claims (2)
０kg/cm2Ｇの加圧力で空気を注入し、１〜４秒間保持溶
解した後ミキシングゾーンにて気泡を発生させ、次いで
同気泡を遠心分離することを特徴とする脱インキ方法。1. The pulp raw material liquid containing recovered waste paper contains 1 to 1
A deinking method comprising injecting air at a pressure of 0 kg / cm 2 G, holding and dissolving for 1 to 4 seconds, generating bubbles in a mixing zone, and then centrifuging the bubbles.
圧注入する手段と、同注入空気の圧力を保持しつつ前記
原料液に注入した空気を溶解させる滞留ゾーンと、同滞
留ゾーンに続き気泡を発生させるミキシングゾーンと、
同ミキシングゾーンで発生した気泡を分離浮上させる遠
心分離ゾーンを設けたことを特徴とする脱インキ装置。2. A means for injecting air into a pulp raw material liquid containing recovered waste paper under pressure, a retention zone for dissolving the air infused into the raw material liquid while maintaining the pressure of the injecting air, and a retention zone following the same. A mixing zone that generates bubbles,
A deinking device comprising a centrifugal separation zone for separating and floating bubbles generated in the mixing zone.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15461093A JPH06346389A (en) | 1993-06-02 | 1993-06-02 | Method for deinking and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15461093A JPH06346389A (en) | 1993-06-02 | 1993-06-02 | Method for deinking and apparatus therefor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06346389A true JPH06346389A (en) | 1994-12-20 |
Family
ID=15587951
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15461093A Withdrawn JPH06346389A (en) | 1993-06-02 | 1993-06-02 | Method for deinking and apparatus therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH06346389A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002294575A (en) * | 2001-03-28 | 2002-10-09 | Ishikawajima Sangyo Kikai Kk | Processing equipment for froth |
| JP2009256808A (en) * | 2008-04-11 | 2009-11-05 | Toppan Printing Co Ltd | Method for recycling waste printed paper |
-
1993
- 1993-06-02 JP JP15461093A patent/JPH06346389A/en not_active Withdrawn
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002294575A (en) * | 2001-03-28 | 2002-10-09 | Ishikawajima Sangyo Kikai Kk | Processing equipment for froth |
| JP4530574B2 (en) * | 2001-03-28 | 2010-08-25 | 株式会社Ｉｈｉ機械システム | Floss processing equipment |
| JP2009256808A (en) * | 2008-04-11 | 2009-11-05 | Toppan Printing Co Ltd | Method for recycling waste printed paper |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A300 | Withdrawal of application because of no request for examination |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 20000905 |